Method for modifying the fluorine distribution in a hydrocarbon compound

ABSTRACT

The present invention relates to a process for modifying the fluorine distribution in a hydrocarbon compound, comprising a step of placing in contact between a hydrocarbon compound and a catalytic composition comprising a chromium-based catalyst, said process being performed in a reactor made of a material comprising a base layer made of a material M1 and an inner layer made of a material M2, said base layer and said inner layer being laid against each other, characterized in that the material M2 comprises at least 80% by weight of nickel on the basis of the total weight of the material M2, advantageously at least 90% by weight, preferably at least 95% by weight, in particular at least 99% by weight of nickel on the basis of the total weight of the material M2.

TECHNICAL FIELD

The present invention relates to processes for modifying the fluorine distribution in the gas phase. In particular, the present invention relates to processes for modifying the fluorine distribution in the gas phase in the presence of a chromium-based catalyst.

TECHNOLOGICAL BACKGROUND OF THE INVENTION

Halogenated hydrocarbons, in particular fluorinated hydrocarbons, such as hydrofluoroolefins, are compounds which have a structure of use as functional materials, solvents, refrigerants, inflating agents and monomers for functional polymers or starting materials for such monomers. Hydrofluoroolefins, such as 2,3,3,3-tetrafluoropropene (HFO-1234yf), are attracting attention because they offer promising behavior as refrigerants having a low global warming potential.

Processes for producing fluoroolefins are usually performed in the presence of a starting substance, such as a chlorine-containing alkane or a chlorine-containing alkene, and in the presence of a fluorinating agent, such as hydrogen fluoride. These processes may be performed in the gas phase or in the liquid phase, in the presence or absence of a catalyst.

The gas-phase processes are usually performed in the presence of catalysts and of hydrofluoric acid. The environment inside the reactor exhibits very high acidity, giving rise to high corrosion of the material of the reactor. The reactors used in processes involving hydrofluoric acid generally comprise a base material and a corrosion-resistant material. The materials used must also have good resistance to high temperature to comply with the requirements in terms of industrial safety.

There is a need for fluorination processes performed in reactors having the various advantages mentioned above.

SUMMARY OF THE INVENTION

The present invention relates to a process for modifying the fluorine distribution in a hydrocarbon compound, comprising a step of placing in contact between a hydrocarbon compound and a catalytic composition comprising a chromium-based catalyst, said process being performed in a reactor made of a material comprising a base layer made of a material M1 and an inner layer made of a material M2, said base layer and said inner layer being laid against each other, characterized in that the material M2 comprises at least 80% by weight of nickel on the basis of the total weight of the material M2, advantageously at least 90% by weight, preferably at least 95% by weight, in particular at least 99% by weight of nickel on the basis of the total weight of the material M2.

According to a preferred embodiment, the material M1 comprises iron and less than 0.2% of carbon on the basis of the total weight of the material M1.

According to a preferred embodiment, the material M2 comprises less than 1% of iron on the basis of the total weight of the material M2.

According to a preferred embodiment, the material M2 comprises less than 1% of manganese on the basis of the total weight of the material M2.

According to a preferred embodiment, the material M2 comprises less than 1% by weight of titanium and/or less than 1% by weight of niobium on the basis of the total weight of the material M2.

According to a preferred embodiment, said hydrocarbon compound is of formula (I) CX(Y)₂—CX(Y)_(m)—CH_(m)XY, in which X and Y independently represent H, F or Cl and m=0 or 1 with at least one from among X or Y which is Cl or F.

According to a preferred embodiment, the hydrocarbon compound is chosen from the group consisting of tetrachloropropene, chlorotrifluoropropene, pentachloropropane, dichlorotrifluoropropane, trichlorodifluoropropane, tetrafluorochloropropane, tetrachlorofluoropropane, dichlorodifluoropropene, trichlorofluoropropene, pentafluoropropane and mixtures thereof; preferably, the hydrocarbon compound is chosen from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene (HFCO-1233xf), 2,3-dichloro-1,1,1-trifluoropropane (HCFC-243db), 1,1,1,2,3-pentachloropropane (HCC-240db), 1,1,2,2,3-pentachloropropane (HCC-240aa), 1,1,1,3,3-pentachloropropane (HCC-240fa), 1,1,2,3-tetrachloro-1-propene (HCO-1230xa), 2,3,3,3-tetrachloro-1-propene (HCO-1230xf), 1,1,3,3-tetrachloro-1-propene (HCO-1230za), 1,3,3,3-tetrachloro-1-propene (HCO-1230zd), 1,1,1,2,2-pentafluoropropane (HFC-245cb) and 1-chloro-3,3,3-trifluoro-1-propene (HCFO-1233zd).

According to a preferred embodiment, the fluorine content of the hydrocarbon compound is increased by reacting said hydrocarbon compound with hydrogen fluoride in the gas phase in the presence of said catalytic composition, the hydrocarbon compound being a saturated halogenated hydrocarbon or an unsaturated halogenated hydrocarbon or an unsaturated hydrocarbon.

According to a preferred embodiment, the fluorine content of the hydrocarbon compound is reduced by dehydrofluorination of said hydrocarbon compound in the presence of said catalytic composition, said hydrocarbon compound being a fluorinated hydrocarbon compound.

According to a preferred embodiment, the fluorine distribution of the hydrocarbon compound is modified by isomerizing said hydrocarbon compound in the presence of said catalytic composition, said hydrocarbon compound being a fluorinated hydrocarbon compound.

According to a preferred embodiment, the fluorine distribution of the hydrocarbon compound is modified by dismutating said hydrocarbon compound in the gas phase in the presence of said catalytic composition, said hydrocarbon compound being a chlorofluorinated hydrocarbon compound.

According to a preferred embodiment, the fluorine content of the hydrocarbon compound is reduced by reacting said hydrocarbon compound with hydrogen chloride in the gas phase in the presence of said catalytic composition, said hydrocarbon compound being a halogenated hydrocarbon compound containing at least one fluorine atom.

According to a preferred embodiment, the fluorine content of a first hydrocarbon compound is increased by reacting said first hydrocarbon compound with hydrogen fluoride in the gas phase in the presence of a catalytic composition comprising a chromium-based catalyst, the first hydrocarbon compound being a saturated halogenated hydrocarbon or an unsaturated halogenated hydrocarbon or an unsaturated hydrocarbon, and the fluorine content of a second hydrocarbon compound is reduced by dehydrofluorinating said second hydrocarbon compound in the presence of said catalytic composition comprising a chromium-based catalyst, said second hydrocarbon compound being a fluorinated hydrocarbon compound.

DETAILED DESCRIPTION OF THE INVENTION

In a first aspect of the present invention, a process for modifying the fluorine distribution in a hydrocarbon compound in the presence of a catalytic composition is provided. In this process, the catalytic composition comprises a chromium-based catalyst. Preferably, the chromium-based catalyst may be a chromium oxide (for example CrO₃ or Cr₂O₃), a chromium oxyfluoride or a chromium fluoride (for example CrF₃) or a mixture thereof. The chromium oxyfluoride may have a fluorine content of between 1% and 60% by weight on the basis of the total weight of the chromium oxyfluoride, advantageously between 5% and 55% by weight, preferably between 10% and 52% by weight, more preferentially between 15% and 52% by weight, in particular between 20% and 50% by weight, more particularly between 25% and 45% by weight, favorably between 30% and 45% by weight, more favorably from 35% to 45% by weight of fluorine on the basis of the total weight of chromium oxyfluoride. The catalyst may also comprise a cocatalyst chosen from the group consisting of Ni, Co, Zn, Mg, Mn, Fe, Zn, Ti, V, Zr, Mo, Ge, Sn, Pb, Sb; preferably Ni, Co, Zn, Mg, Mn; in particular Ni, Co, Zn. The weight content of the cocatalyst is between 1% and 10% by weight on the basis of the total weight of the catalytic composition. The catalytic composition may also comprise a support such as alumina, for example in its alpha form, activated alumina, aluminum halides (for example AlF₃), aluminum oxyhalides, active charcoal, magnesium fluoride or graphite. Preferably, the catalytic composition has a specific surface area of between 1 and 100 m²/g, preferably between 5 and 80 m²/g, more preferentially between 5 and 70 m²/g, ideally between 5 and 50 m²/g, in particular between 10 and 50 m²/g, more particularly between 15 and 45 m²/g.

The catalysts provided according to the present invention may be used to modify the fluorine distribution in hydrocarbon compounds, the latter being halogenated or non-halogenated hydrocarbon compounds. The fluorine distribution in a hydrocarbon compound can be modified by increasing the fluorine content of the hydrocarbon compound. The fluorine distribution of a hydrocarbon compound can also be modified by reducing the fluorine content of the hydrocarbon compound and/or by rearranging the position of fluorine atoms on the carbon atoms of the hydrocarbon compound.

The present invention can provide processes in which the fluorine distribution in hydrocarbon compounds containing between one and twelve carbon atoms is modified, preferably processes in which the fluorine distribution in hydrocarbon compounds containing between one and six carbon atoms is modified, in particular processes in which the fluorine distribution in hydrocarbon compounds containing three carbon atoms is modified, more particularly in which the fluorine distribution in halogenated hydrocarbon compounds containing three carbon atoms is modified. The present invention can provide processes in which the fluorine content of hydrocarbon compounds containing between one and twelve carbon atoms is increased, preferably processes in which the fluorine content of hydrocarbon compounds containing between one and six carbon atoms is increased, in particular processes in which the fluorine content of hydrocarbon compounds containing three carbon atoms is increased, more particularly processes in which the fluorine content of halogenated hydrocarbon compounds containing three carbon atoms is increased. The processes for modifying the fluorine distribution of hydrocarbon compounds, preferably of halogenated hydrocarbon compounds, include fluorination, chlorofluorination, isomerization, dismutation, dehydrofluorination and chlorodefluorination.

The hydrocarbon compounds include those of general formula C_(h)H_(a)Br_(b)Cl_(c)F_(d), in which h is an integer between 1 and 6, a is an integer between 0 and 13, b is an integer between 0 and 4, c is an integer between 0 and 13, d is an integer between 0 and 13, and the sum of a, b, c and d is equal to 2h+2; or those of general formula C_(p)H_(e)Br_(f)Cl_(g)F_(h), in which p is an integer between 2 and 6, e is an integer between 0 and 10, f is an integer between 0 and 2, g is an integer between 0 and 12, h is an integer between 0 and 11, and the sum of e, f, g and h is equal to 2p. Preferably, the hydrocarbon compounds include those of general formula C_(h)H_(a)Cl_(c)F_(d), in which h is an integer between 2 and 4, a is an integer between 0 and 9, c is an integer between 0 and 9, d is an integer between 0 and 9, and the sum of a, c and d is equal to 2h+2; or those of general formula C_(p)H_(e)Cl_(g)F_(h), in which p is an integer between 2 and 4, e is an integer between 0 and 8, g is an integer between 0 and 8, h is an integer between 0 and 7, and the sum of e, f, g and h is equal to 2p.

In particular, the hydrocarbon compounds that are suitable for use in the processes according to the present invention are of formula (I) CX(Y)₂—CX(Y)_(m)—CH_(m)XY, in which X and Y independently represent H, F or Cl and m=0 or 1 with at least one from X or Y being Cl or F.

Preferably, the hydrocarbon compounds may be chosen from the group consisting of tetrachloropropene, chlorotrifluoropropene, pentachloropropane, dichlorotrifluoropropane, trichlorodifluoropropane, tetrachlorofluoropropane, dichlorodifluoropropene, trichlorofluoropropene, pentafluoropropane, chloroterafluoropropane and mixtures thereof.

Preferably, the hydrocarbon compounds may be chosen from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene (HFCO-1233xf), 2,3-dichloro-1,1,1-trifluoropropane (HCFC-243db), 1,1,1,2,3-pentachloropropane (HCC-240db), 1,1,2,2,3-pentachloropropane (HCC-240aa), 1,1,1,3,3-pentachloropropane (HCC-240fa), 1,1,2,3-tetrachloro-1-propene (HCO-1230xa), 2,3,3,3-tetrachloro-1-propene (HCO-1230xf), 1,1,3,3-tetrachloro-1-propene (HCO-1230za), 1,3,3,3-tetrachloro-1-propene (HCO-1230zd), 1,1,1,2,2-pentafluoropropane (HFC-245cb) and 1-chloro-3,3,3-trifluoro-1-propene (HCFO-1233zd).

Said process according to the present invention is performed in a reactor made of a material comprising a base layer made of a material M1 and an inner layer made of a material M2, said base layer and said inner layer being laid against each other. The reactor may be a reactor with a fixed catalytic bed or a reactor with a fluidized catalytic bed or a multitubular reactor. Preferably, said reactor is a reactor with a fixed catalytic bed.

According to a preferred embodiment, the degree of corrosion of the material M2 is less than 1 mm/year, advantageously less than 0.5 mm/year, preferably less than 0.1 mm/year, more preferentially less than 0.05 mm/year, in particular less than 0.025 mm/year, more particularly less than 10 μm/year, favorably less than 5 μm/year. This degree is measured according to the coupon method ASTM D 2 328-65 T.

The inner layer is the layer in contact with the hydrocarbon compound. The inner layer is also in contact with the other starting materials used, for example the hydrofluoric acid, and the products generated during the reaction performed in the reactor.

According to a preferred embodiment, said base layer and said inner layer are laid against each other by bonding. Preferably, the bonding is performed by weld bonding, explosive bonding, hot roll bonding or cold roll bonding. Preferably, the bonding is performed by explosive bonding or by hot roll bonding. In particular, the bonding is performed by explosive bonding.

The material M2 is in contact with the hydrocarbon compound. Preferably, the material M2 may have a tensile strength lower than that of the material M1. The material M2 may also have an elongation greater than that of the material M1.

According to a preferred embodiment, said inner layer has a thickness of between 0.01 and 20 mm, said thickness of said inner layer being less than that of said base layer. Preferably, said inner layer may have a thickness of between 0.05 and 15 mm, preferably between 0.1 and 10 mm and more preferentially between 0.1 and 5 mm.

Advantageously, the material M2 comprises at least 80% by weight of nickel on the basis of the total weight of the material M2. Preferably, the material M2 comprises at least 85% by weight of nickel, more preferentially at least 90% by weight of nickel, in particular at least 95% by weight of nickel, more particularly at least 99% by weight of nickel on the basis of the total weight of the material M2. Thus, the material M2 may comprise at least 80%, at least 81%, at least 82%, at least 83%, at least 84%, at least 85%, at least 86%, at least 87%, at least 88%, at least 89%, at least 90%, at least 91%, at least 92%, at least 93%, at least 94%, at least 95%, at least 96%, at least 97%, at least 98% or at least 99% by weight of nickel on the basis of the total weight of the material M2.

The material M2 may also comprise iron in a content of less than 1% by weight on the basis of the total weight of the material M2, advantageously less than 0.9% by weight, preferably less than 0.8% by weight, more preferentially less than 0.7% by weight, in particular less than 0.6% by weight, more particularly less than 0.5% by weight on the basis of the total weight of the material M2. Preferably, the material M2 comprises between 0.1% and 1% by weight of iron, in particular between 0.3% and 0.8% by weight of iron, more particularly between 0.3% and 0.5% by weight of iron on the basis of the total weight of the material M2.

The material M2 may also comprise manganese in a content of less than 7% by weight on the basis of the total weight of the material M2, advantageously less than 6% by weight, preferably less than 5% by weight, more preferentially less than 4% by weight, in particular less than 3% by weight, more particularly less than 2% by weight, favorably less than 1% by weight, preferentially favorably less than 0.75%, particularly favorably less than 0.5% on the basis of the total weight of the material M2. Preferably, the material M2 comprises between 0.1% and 1% by weight of manganese, in particular between 0.3% and 0.8% by weight of manganese, more particularly between 0.3% and 0.5% by weight of manganese on the basis of the total weight of the material M2. Alternatively, the material M2 comprises between 3% and 7% by weight of manganese, in particular between 3.5% and 6.5% by weight of manganese, more particularly between 4% and 6% by weight of manganese on the basis of the total weight of the material M2.

The material M2 may also comprise silicon in a content of less than 1% by weight on the basis of the total weight of the material M2, advantageously less than 0.9% by weight, preferably less than 0.8% by weight, more preferentially less than 0.7% by weight, in particular less than 0.6% by weight, more particularly less than 0.5% by weight on the basis of the total weight of the material M2. Preferably, the material M2 comprises between 0.1% and 1% by weight of silicon, in particular between 0.3% and 0.8% by weight of silicon, more particularly between 0.3% and 0.5% by weight of silicon on the basis of the total weight of the material M2. Alternatively, the material M2 comprises between 0.05% and 0.5% by weight of silicon, in particular between 0.1% and 0.3% by weight of silicon, more particularly between 0.1% and 0.25% by weight of silicon on the basis of the total weight of the material M2.

The material M2 may also comprise copper in a content of less than 1% by weight on the basis of the total weight of the material M2, advantageously less than 0.9% by weight, preferably less than 0.8% by weight, more preferentially less than 0.7% by weight, in particular less than 0.6% by weight, more particularly less than 0.5% by weight, favorably less than 0.4% by weight, particularly favorably less than 0.3% by weight on the basis of the total weight of the material M2. Preferably, the material M2 comprises between 0.1% and 1% by weight of copper, in particular between 0.2% and 0.5% by weight of copper, more particularly between 0.2% and 0.3% by weight of copper on the basis of the total weight of the material M2.

The material M2 may also comprise carbon in a content of less than 0.1% by weight on the basis of the total weight of the material M2, advantageously less than 0.09% by weight, preferably less than 0.08% by weight, more preferentially less than 0.07% by weight, in particular less than 0.06% by weight, more particularly less than 0.05% by weight, favorably less than 0.04% by weight, particularly favorably less than 0.03% by weight on the basis of the total weight of the material M2. Preferably, the material M2 comprises between 0.005% and 0.1% by weight of carbon, in particular between 0.01% and 0.075% by weight of carbon, more particularly between 0.01% and 0.05% by weight of carbon on the basis of the total weight of the material M2.

The material M2 may comprise less than 0.1% by weight of sulfur on the basis of the total weight of the material M2, advantageously less than 0.09% by weight, preferably less than 0.08% by weight, more preferentially less than 0.07% by weight, in particular less than 0.06% by weight, more particularly less than 0.05% by weight, favorably less than 0.04% by weight, particularly favorably less than 0.03% by weight, more particularly favorably less than 0.02% by weight of sulfur on the basis of the total weight of the material M2.

The material M2 may comprise less than 1% by weight of titanium on the basis of the total weight of the material M2, advantageously less than 0.5% by weight of titanium, preferably less than 0.1% by weight of titanium, more preferentially less than 0.05% by weight of titanium, in particular less than 0.01% by weight of titanium on the basis of the total weight of the material M2; favorably, the material M2 is free of titanium.

The material M2 may comprise less than 1% by weight of niobium, advantageously less than 0.5% by weight of niobium, preferably less than 0.1% by weight of niobium, more preferentially less than 0.05% by weight of niobium, in particular less than 0.01% by weight of niobium on the basis of the total weight of the material M2; favorably, the material M2 is free of niobium.

According to a preferred embodiment, the material M1 comprises at least 70% by weight of iron, advantageously at least 75% by weight, preferably at least 80% by weight, more preferentially at least 85% by weight, in particular at least 90% by weight, more particularly at least 95% by weight of iron on the basis of the total weight of the material M1.

The material M1 may also comprise less than 2% by weight of carbon, advantageously less than 1.5% by weight, preferably less than 1% by weight, more preferentially less than 0.75% by weight, in particular less than 0.5% by weight, more particularly less than 0.2% by weight, favorably less than 0.1% by weight on the basis of the total weight of the material M1. More particularly, the material M1 may comprise between 0.01% and 0.2% by weight of carbon on the basis of the total weight of the material M1.

The material M1 may also comprise less than 2% by weight of molybdenum, advantageously less than 1.5% by weight, preferably less than 1.25% by weight, more preferentially less than 1% by weight of molybdenum on the basis of the total weight of the material M1. More particularly, the material M1 may comprise between 0.1% and 1% by weight of molybdenum on the basis of the total weight of the material M1.

The material M1 may also comprise less than 5% by weight of chromium, advantageously less than 4% by weight, preferably less than 3% by weight, more preferentially less than 2% by weight, in particular less than 1% by weight of chromium on the basis of the total weight of the material M1. More particularly, the material M1 may comprise between 0.5% and 2% by weight of chromium on the basis of the total weight of the material M1.

The material M1 may also comprise less than 2% by weight of silicon, advantageously less than 1.5% by weight, preferably less than 1.25% by weight, more preferentially less than 1% by weight of silicon on the basis of the total weight of the material M1. More particularly, the material M1 may comprise between 0.1% and 1.5% by weight of silicon on the basis of the total weight of the material M1.

The material M1 may also comprise less than 2% by weight of manganese, advantageously less than 1.5% by weight, preferably less than 1.25% by weight, more preferentially less than 1% by weight of manganese on the basis of the total weight of the material M1. More particularly, the material M1 may comprise between 0.1% and 1% by weight of manganese on the basis of the total weight of the material M1.

Thus, the reactor used in the processes according to the invention comprises a base layer made of a material M1 and an inner layer, in contact with at least the hydrocarbon compound, made of a material M2 laid against each other; said material M2 comprising:

-   -   at least 80% by weight of nickel, preferably at least 85% by         weight of nickel, more preferentially at least 90% by weight of         nickel, in particular at least 95% by weight of nickel, more         particularly at least 99% by weight of nickel on the basis of         the total weight of the material M2; and less than 1% by weight         of iron on the basis of the total weight of the material M2,         advantageously less than 0.9% by weight, preferably less than         0.8% by weight, more preferentially less than 0.7% by weight, in         particular less than 0.6% by weight, more particularly less than         0.5% by weight of iron on the basis of the total weight of the         material M2; and/or less than 7% by weight of manganese,         advantageously less than 6% by weight, preferably less than 5%         by weight, more preferentially less than 4% by weight, in         particular less than 3% by weight, more particularly less than         2% by weight, favorably less than 1% by weight, preferentially         favorably less than 0.75%, particularly favorably less than 0.5%         by weight of manganese on the basis of the total weight of the         material M2; and/or less than 1% by weight of silicon,         advantageously less than 0.9% by weight, preferably less than         0.8% by weight, more preferentially less than 0.7% by weight, in         particular less than 0.6% by weight, more particularly less than         0.5% by weight of silicon on the basis of the total weight of         the material M2; and/or less than 1% by weight of copper,         advantageously less than 0.9% by weight, preferably less than         0.8% by weight, more preferentially less than 0.7% by weight, in         particular less than 0.6% by weight, more particularly less than         0.5% by weight, favorably less than 0.4% by weight, particularly         favorably less than 0.3% by weight of copper on the basis of the         total weight of the material M2; and/or less than 0.1% by weight         of carbon, advantageously less than 0.09% by weight, preferably         less than 0.08% by weight, more preferentially less than 0.07%         by weight, in particular less than 0.06% by weight, more         particularly less than 0.05% by weight, favorably less than         0.04% by weight, particularly favorably less than 0.03% by         weight of carbon on the basis of the total weight of the         material M2; and/or less than 0.1% by weight of sulfur,         advantageously less than 0.09% by weight, preferably less than         0.08% by weight, more preferentially less than 0.07% by weight,         in particular less than 0.06% by weight, more particularly less         than 0.05% by weight, favorably less than 0.04% by weight,         particularly favorably less than 0.03% by weight, more         particularly favorably less than 0.02% by weight of sulfur on         the basis of the total weight of the material M2; and/or     -   less than 4% by weight of titanium, advantageously less than 3%         by weight, preferably less than 2% by weight, more         preferentially less than 1% by weight, in particular less than         0.5% by weight of titanium, more particularly less than 0.05% by         weight of titanium on the basis of the total weight of the         material M2; favorably, the material M2 is free of titanium;         and/or     -   less than 1% by weight of niobium, advantageously less than 0.5%         by weight of niobium, preferably less than 0.1% by weight of         niobium, more preferentially less than 0.05% by weight of         niobium, in particular less than 0.01% by weight of niobium on         the basis of the total weight of the material M2; favorably, the         material M2 is free of niobium; and     -   the material M1 comprising at least 70% by weight of iron,         advantageously at least 75% by weight, preferably at least 80%         by weight, more preferentially at least 85% by weight, in         particular at least 90% by weight, more particularly at least         95% by weight of iron on the basis of the total weight of the         material M1; and less than 2% by weight of carbon,         advantageously less than 1.5% by weight, preferably less than 1%         by weight, more preferentially less than 0.75% by weight, in         particular less than 0.5% by weight, more particularly less than         0.2% by weight, favorably less than 0.1% by weight on the basis         of the total weight of the material M1, more particularly         between 0.01% and 0.2% by weight of carbon on the basis of the         total weight of the material M1 and less than 2% by weight of         molybdenum, advantageously less than 1.5% by weight, preferably         less than 1.25% by weight, more preferentially less than 1% by         weight of molybdenum on the basis of the total weight of the         material M1, more particularly between 0.1% and 1% by weight of         molybdenum on the basis of the total weight of the material M1;         and/or less than 5% by weight of chromium, advantageously less         than 4% by weight, preferably less than 3% by weight, more         preferentially less than 2% by weight, in particular less than         1% by weight of chromium on the basis of the total weight of the         material M1, more particularly between 0.5% and 2% by weight of         chromium on the basis of the total weight of the material M1.

Preferably, the reactor is fed with hydrocarbon compound via feed lines. The reactor also comprises effluent or outlet lines for removing the reaction mixture from the reactor.

Preferably, the feed or outlet lines of the reactor are made of a specific material that is also capable of withstanding corrosion, for example made of the material M2. The feed lines may be of tubular shape. Alternatively, the feed or outlet lines may be made of a material comprising a base layer made of a material M1 covered with an inner layer, in contact with the hydrocarbon or another starting material, for example HF, made of a material M2.

The reactor also comprises one or more dephlegmators, one or more dip tubes, one or more devices for introducing the starting materials, and one or more gratings for supporting and retaining the catalyst. Said one or more dephlegmators and/or said one or more dip tubes and/or said one or more devices for introducing the starting materials and/or said one or more gratings for supporting and retaining the catalyst may be made of a material comprising a base layer made of a material M1 covered with an inner layer, in contact with the hydrocarbon or another starting material, for example HF, made of a material M2. The materials M1 and M2 are as described above.

In a first embodiment, the fluorine content of the hydrocarbon compound is increased by reacting said compound with hydrogen fluoride in the presence of said catalytic composition, the hydrocarbon compound being a saturated halogenated hydrocarbon or an unsaturated halogenated hydrocarbon or an unsaturated hydrocarbon. A hydrocarbon compound is halogenated when it comprises at least one halogen. A hydrocarbon is unsaturated when it contains at least one carbon-carbon double bond.

Hydrocarbon compounds that are suitable as starting reagents for the fluorination process of this first embodiment may be saturated or unsaturated halogenated hydrocarbon compounds. The saturated halogenated hydrocarbon compounds include those of general formula C_(h)H_(a)Br_(b)Cl_(c)F_(d), in which h is an integer between 1 and 6, a is an integer between 0 and 13, b is an integer between 0 and 4, c is an integer between 0 and 13, d is an integer between 0 and 13, provided that b+c is at least equal to 1 and the sum of a, b, c and d is equal to 2h+2. Preferably, the saturated halogenated hydrocarbon compounds include those of general formula C_(h)H_(a)Cl_(c)F_(d), in which h is an integer between 2 and 4, a is an integer between 0 and 9, c is an integer between 1 and 9, d is an integer between 0 and 9, and the sum of a, c and d is equal to 2h+2. The unsaturated halogenated hydrocarbon compounds include those of general formula C_(p)H_(e)Br_(f)Cl_(g)F_(h), in which p is an integer between 2 and 6, e is an integer between 0 and 11, f is an integer between 0 and 2, g is an integer between 0 and 12, h is an integer between 0 and 11, provided that f+g is at least equal to 1, and the sum of e, f, g and h is equal to 2p. Preferably, the unsaturated halogenated hydrocarbon compounds include those of general formula C_(p)H_(e)Cl_(g)F_(h), in which p is an integer between 2 and 4, e is an integer between 0 and 7, g is an integer between 1 and 8, h is an integer between 0 and 7, and the sum of e, g and h is equal to 2p. The fluorine content of the saturated halogenated hydrocarbon compounds of formula C_(h)H_(a)Br_(b)Cl_(c)F_(d), of the unsaturated halogenated hydrocarbon compounds of formula C_(p)H_(e)Br_(f)Cl_(g)F_(h), as defined above, may be increased by reacting said hydrocarbon compounds with HF in the vapor phase in the presence of said catalytic composition.

The process according to the first embodiment may be performed in a reactor according to the present invention comprising a catalytic bed containing said catalytic composition and according to the following operating conditions:

-   -   an HF/hydrocarbon compound mole ratio between 1:1 and 150:1,         preferably between 2:1 and 125:1, more preferentially between         3:1 and 100:1;     -   a contact time between 1 and 100 s, preferably between 2 and 75         s, in particular between 3 and 50 s;     -   a pressure between atmospheric pressure and 20 bara, preferably         between 2 and 18 bara, more preferentially between 3 and 15         bara;     -   a temperature, preferably of the catalytic bed, between 200 and         450° C., preferably between 250 and 400° C., more preferentially         between 280° C. and 380° C.

The process may be successfully performed over a time of between 10 and 8000 hours, preferably between 50 and 5000 hours, more preferentially between 70 and 1000 hours.

An oxidant, such as oxygen or chlorine, may be added during the process. The mole ratio of the oxidant to the hydrocarbon compound may be between 0.005 and 2, preferably between 0.01 and 1.5. The oxidant may be pure oxygen, air, or a mixture of oxygen and nitrogen.

The amount of HF reacted with the hydrocarbon compounds has to be at least stoichiometric. The stoichiometric amount is based on the number of Br and/or Cl substituents to be replaced with F, in addition to one mole of HF to saturate the carbon-carbon double bond(s), if any.

Examples of saturated halogenated compounds of formula C_(n)H_(a)Br_(b)Cl_(c)F_(d) that may be reacted with HF in the presence of the catalysts of this invention include CH₂Cl₂, CH₂Br₂, CHCl₃, CCl₄, C₂Cl₆, C₂BrCl₅, C₂Cl₅F, C₂Cl₄F₂, C₂Cl₃F₃, C₂Cl₂F₄, C₂ClF₅, C₂HCl₅, C₂HCl₄F, C₂HCl₃F₂, C₂HCl₂F₃, C₂HClF₄, C₂HBrF₄, C₂H₂Cl₄, C₂H₂Cl₃F, C₂H₂Cl₂F₂, C₂H₂ClF₃, C₂H₃Cl₃, C₂H₃Cl₂F, C₂H₃ClF₂, C₂H₄Cl₂, C₂H₄ClF, C₃Cl₆F₂, C₃Cl₅F₃, C₃Cl₄F₄, C₃Cl₃F₅, C₃HCl₇, C₃HCl₆F, C₃HCl₅F₂, C₃HCl₄F₃, C₃HCl₃F₄, C₃HCl₂F₅, C₃Cl₂F₆, C₃H₂Cl₆, C₃H₂BrCl₅, C₃H₂Cl₅F, C₃H₂Cl₄F₂, C₃H₂Cl₃F₃, C₃H₂Cl₂F₄, C₃H₂ClF₅, C₃H₃Cl₅, C₃H₃Cl₄F, C₃H₃Cl₃F₂, C₃H₃Cl₂F₃, C₃H₃ClF₄, C₃H₄Cl₄, C₄Cl₄Cl₄, C₄Cl₄Cl₆, C₄H₆Cl₆, C₄H₅Cl₄F₁ and C₆H₄Cl₈.

Specific examples of fluorination reactions of saturated halogenated hydrocarbon compounds that may be successfully performed under the conditions described above using the catalysts of this invention include the conversion of 1,1,2-trichloroethane (CHCl₂CH₂Cl or HCC-140) into 1-chloro-2,2-difluoroethane (CH₂ClCF₂H or HCFC-142), the conversion of 1,1,1,3,3,3-hexachlorodifluoropropane (CCl₃CF₂CCl₃ or CFC-212ca) into a mixture of 1,1,3-trichloro-1,2,2,3,3-pentafluoropropane (CCl₂FCF₂CClF₂ or CFC-215ca) and 1,3-dichloro-1,1,2,2,3,3-hexafluoropropane (CClF₂CF₂CClF₂ or CFC-216ca), the conversion of 1,1,1,3,3,3-hexachloropropane (CCl₃CH₂CCl₃ or HCC-230fa) into 1-chloro-1,1,3,3,3-pentafluoropropane (CF₃CH₂CClF₂ or HCFC-235fa) and 1,1,1,3,3,3-hexafluoropropane (CF₃CH₂CF₃ or HFC-236fa), the conversion of 1,1,1,3,3-pentachloropropane (CCl₃CH₂CHCl₂ or HCC-240fa) into a mixture of 1,1,1,3,3-pentafluoropropane (CHF₂CH₂CF₃ or HFC-245fa), 1-chloro-3,3,3-trifluoro-1-propene (CHCl═CHCF₃ or HCFO-1233zd) and 1,3,3,3-tetrafluoropropene (CHF═CHCF₃ or HFO-1234ze), the conversion of 2,2,3-trichloro-1,1,1,3,3-pentafluoropropane (CF₃CCl₂CClF₂ or CFC-215aa) into a mixture of 1,1,1,3,3,3-hexachlorodifluoropropane (CF₃CCl₂CF₃ or CFC-216ca) and 2-chloro-1,1,1,2,3,3,3-heptafluoropropane (CF₃CClFCF₃ or CFC-217ba), the conversion of 1,1,1,3,3,3-hexachlorodifluoropropane (CF₃CCl₂CF₃ or CFC-216ca) into 2-chloro-1,1,1,2,3,3,3-heptafluoropropane (CF₃ClFCF₃ or CFC-217ba), the conversion of a mixture containing 1,1-dichloro-2,2,3,3,3-pentafluoropropane (CF₃CF₂CHCl₂ or HCFC-225ca) and 1,3-dichloro-1,2,2,3,3-pentafluoropropane (CClF₂CF₂CHClF or HCFC-225cb) into a mixture of 1-chloro-1,2,2,3,3,3-hexafluoropropane (CF₃CF₂CHClF or HCFC-226ca) and 1,1,1,2,2,3,3-heptafluoropropane (CF₃CF₂CHF₂ or HFC-227ca), the conversion of 1,1,1,2,3-pentachloropropane (CCl₃CHClCH₂Cl or HCC-240db) into 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf), the conversion of 1,1,2,2,3-pentachloropropane (CHCl₂CCl₂CH₂Cl or HCC-240aa) into 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf), the conversion of 1,1,1,2,3-pentachloropropane (CCl₃CHClCH₂Cl or HCC-240db) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), the conversion of 1,1,2,2,3-pentachloropropane (CHCl₂CCl₂CH₂Cl or HCC-240aa) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), the conversion of 1,1,1,3,3-pentachloropropane (CCl₃CH₂CHCl₂ or HCC-240fa) into 1,3,3,3-tetrafluoropropene (CF₃CH═CHF or HFO-1234ze), in particular the conversion of 1,1,1,2,3-pentachloropropane (CCl₃CHClCH₂Cl or HCC-240db) into 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf), the conversion of 1,1,2,2,3-pentachloropropane (CHCl₂CCl₂CH₂Cl or HCC-240aa) into 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf), the conversion of 1,1,1,2,3-pentachloropropane (CCl₃CHClCH₂Cl or HCC-240db) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), the conversion of 1,1,2,2,3-pentachloropropane (CHCl₂CCl₂CH₂Cl or HCC-240aa) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), the conversion of 1,1,1,3,3-pentachloropropane (CCl₃CH₂CHCl₂ or HCC-240fa) into 1,3,3,3-tetrafluoropropene (CF₃CH═CHF or HFO-1234ze), the conversion of 1,1,2-trichloroethane (CHCl₂CH₂Cl or HCC-140) into 1-chloro-2,2-difluoroethane (CH₂ClCF₂H or HCFC-142).

Examples of unsaturated halogenated or non-halogenated compounds of formulae C_(p)H_(e)Br_(f)Cl_(g)F_(h) and C_(i)H_(i) which may be reacted with HF in the presence of the catalysts of this invention include C₂Cl₄, C₂BrCl₃, C₂Cl₃F, C₂Cl₂F₂, C₂ClF₃, C₂F₄, C₂HCl₃, C₂HBrCl₂, C₂HCl₂F, C₂HClF₂, C₂HF₃, C₂H₂Cl₂, C₂H₂ClF, C₂H₂F₂, C₂H₃Cl, C₂H₃F, C₂H₄, C₃H₆, C₃H₅Cl, C₃H₄Cl₂, C₃H₃Cl₃, C₃H₂Cl₄, C₃HCl₅, C₃H₂ClF₃, C₃F₃HCl₂, C₃F₂H₂Cl₂, C₃F₄H, ClC₃Cl₆, C₃Cl₅F, C₃Cl₄F₂, C₃Cl₃F₃, C₃Cl₂F₄, C₃ClF₅, C₃HF₅, C₃H₂F₄, C₃F₆, C₄Cl₈, C₄Cl₂F₆, C₄ClF₇, C₄H₂F₆ and C₄HClF₆.

Specific examples of fluorination reactions of unsaturated halogenated hydrocarbon compounds that may be successfully performed using the catalysts of this invention include the conversion of 1,2-dichloroethylene (CHCl═CClH or HCO-1130) into 1-chloro-2,2-difluoroethane (CH₂ClCF₂H or HCFC-142), the conversion of 1,1,2-trichloro-3,3,3-trifluoro-1-propene (CCl₂═CClCF₃ or CFC-1213xa) into a mixture of 2,3-dichloro-1,1,1,3,3-pentafluoropropane (CF₃CHClCClF₂ or HCFC-225da), 2-chloro-1,1,1,3,3,3-hexafluoropropane (CF₃CHClCF₃ or HCFC-226da) and/or 2-chloro-1,1,3,3,3-pentafluoro-1-propene (CF₃CCl═CF₂ or CFC-1215xc), the conversion of hexafluoropropene (CF₃CF═CF₂ or CFC-1216yc) into 1,1,1,2,3,3,3-heptafluoropropane (CF₃CHFCF₃ or HFC-227ea), the conversion of 1,1,3,3,3-pentafluoropropene (CF₃CH═CF₂ or HFO-1225zc) into 1,1,1,3,3,3-hexafluoropropane (CF₃CH₂CF₃ or HFC-236fa), the conversion of 1,3,3,3-tetrafluoropropene (CF₃CH═CHF or HFO-1234ze) into 1,1,1,3,3-pentafluoropropane (CF₃CH₂CHF₂ or HFC-245fa), the conversion of 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), the conversion of 1,1,2,3-tetrachloro-1-propene (CCl₂═CClCH₂Cl or HCO-1230xa) into 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf) or 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), the conversion of 2,3,3,3-tetrachloro-1-propene (CCl₃CCl═CH₂ or HCO-1230xf) into 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf) or into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), the conversion of 1-chloro-3,3,3-trifluoro-1-propene (CF₃CH═CHCl or HCFO-1233zd) or 1,1,3,3-tetrachloro-1-propene (CCl₂═CHCHCl₂ or HCO-1230za) or 1,3,3,3-tetrachloroprop-1-ene (CCl₃CH═CHCl or HCO-1230zd) into 1,3,3,3-tetrafluoropropene (CF₃CH═CHF or HFO-1234ze), in particular the conversion of 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), the conversion of 1,1,2,3-tetrachloro-1-propene (CCl₂═CClCH₂Cl or HCO-1230xa) into 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf) or into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), the conversion of 2,3,3,3-tetrachloro-1-propene (CCl₃Cl═CH₂ or HCO-1230xf) into 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf) or into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), the conversion of 1,1,3,3-tetrachloro-1-propene (CCl₂═CHCHCl₂ or HCO-1230za) or 1,3,3,3-tetrachloroprop-1-ene (CCl₃CH═CHCl or HCO-1230zd) into 1-chloro-3,3,3-trifluoro-1-propene (CF₃CH═CHCl or HCFO-1233zd), the conversion of 1-chloro-3,3,3-trifluoro-1-propene (CF₃CH═CHCl or HCFO-1233zd) or 1,1,3,3-tetrachloro-1-propene (CCl₂═CHCHCl₂ or HCO-1230za) or 1,3,3,3-tetrachloroprop-1-ene (CCl₃CH═CHCl or HCO-1230zd) into 1,3,3,3-tetrafluoropropene (CF₃CH═CHF or HFO-1234ze), the conversion of 1,2-dichloroethylene (CHCl═CClH or HCO-1130) into 1-chloro-2,2-difluoroethane (CH₂ClCF₂H or HCFC-142).

Preferentially, the hydrocarbon compound is chosen from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene (HFCO-1233xf), 1,1,1,2,3-pentachloropropane (HCC-240db), 1,1,2,2,3-pentachloropropane (HCC-240aa), 1,1,2,3-tetrachloro-1-propene (HCO-1230xa), 2,3,3,3-tetrachloro-1-propene (HCO-1230xf), or mixtures thereof, for the production of 2,3,3,3-tetrafluoropropene (HFO-1234yf).

Otherwise, the hydrocarbon compound is chosen from the group consisting of 1-chloro-3,3,3-trifluoro-1-propene (HCFO-1233zd), 1,1,1,3,3-pentachloropropane (HCC-240fa), 1,1,3,3-tetrachloro-1-propene (HCO-1230za), 1,3,3,3-tetrachloro-1-propene (HCO-1230zd), or mixtures thereof, for the production of 1,3,3,3-tetrafluoropropene (HFO-1234ze).

In a second embodiment, the fluorine content of the hydrocarbon compound is reduced by dehydrofluorinating said hydrocarbon compound in the presence of said catalytic composition, said hydrocarbon compound being a fluorinated hydrocarbon compound.

The fluorinated hydrocarbon compounds that are suitable as starting materials in the dehydrofluorination process of this invention are typically saturated. The saturated halogenated hydrocarbon compounds include those of general formula C_(n)H_(a)Cl_(c)F_(d), in which n is an integer between 2 and 6, a is an integer between 1 and 13, c is an integer between 0 and 12, d is an integer between 1 and 13, and the sum of a, c and d is equal to 2n+2. Preferably, the saturated halogenated hydrocarbon compounds include those of general formula C_(n)H_(a)Cl_(c)F_(d), in which n is an integer between 2 and 4, a is an integer between 1 and 9, c is an integer between 0 and 6, d is an integer between 1 and 9, and the sum of a, c and d is equal to 2n+2. The fluorine content of the saturated compounds of formula C_(n)H_(a)F_(d) may be reduced in the presence of said catalytic composition.

The process according to the second embodiment may be performed in a reactor comprising a catalytic bed containing a catalyst and according to the following operating conditions:

-   -   an HF/hydrocarbon compound mole ratio between 1:1 and 150:1,         preferably between 2:1 and 125:1, more preferentially between         3:1 and 100:1;     -   a contact time between 1 and 100 s, preferably between 2 and 75         s, in particular between 3 and 50 s;     -   a pressure between atmospheric pressure and 20 bara, preferably         between 2 and 18 bara, more preferentially between 3 and 15         bara;     -   a temperature, preferably of the catalytic bed, between 200 and         450° C., preferably between 250 and 400° C., more preferentially         between 280° C. and 380° C.

The process may be successfully performed over a time of between 10 and 8000 hours, preferably between 50 and 5000 hours, more preferentially between 70 and 1000 hours.

An oxidant, such as oxygen or chlorine, may be added during the process. The mole ratio of the oxidant to the hydrocarbon compound may be between 0.005 and 2, preferably between 0.01 and 1.5. The oxidant may be pure oxygen, air, or a mixture of oxygen and nitrogen.

The product of the dehydrofluorination reaction consists of HF and of the unsaturated fluorinated hydrocarbon compound resulting from the loss of HF by the initial reagent. Specific examples of gas-phase dehydrofluorination reactions which may be performed using the catalysts of this invention include the conversion of 1,1-difluoroethane (CHF₂CH₃ or HFC-152a) into vinyl chloride (CHF═CH₂ or HFO-1141), the conversion of 1,1,1-trifluoroethane (CF₃CH₃ or HFC-143a) into vinylidene fluoride (CF₂═CH₂ or HFO-1132a), the conversion of 2-chloro-1,1,1-trifluoroethane (CF₃CH₂Cl or HCFC-133a) into 2-chloro-1,1-difluoroethylene (CF₂═CHCl or HCFO-1122), the conversion of 1,1,1,2-tetrafluoroethane (CF₃CH₂F or HFC-134a) into trifluoroethylene (CF₂═CHF or HFO-1123), the conversion of 1,1,2,2-tetrafluoroethane (CHF₂CHF₂ or HFC-134) into trifluoroethylene (CF₂═CHF or HFO-1123), the conversion of 1,1,1,2-tetrafluoropropane (CH₃CHFCF₃ or HFC-254eb) into 1,1,1-trifluoropropene (CH₂═CHCF₃ or HFO-1243zf), the conversion of 1,1,1,3,3-pentafluoropropane (CHF₂CH₂CF₃ or HFC-245fa) into 1,3,3,3-tetrafluoropropene (CHF═CHCF₃ or HFO-1234ze), the conversion of 1,1,1,2,3,3-hexafluoropropane (CHF₂CHFCF₃ or HFC-236ea) into 1,2,3,3,3-pentafluoropropene (CHF═CFCF₃ or HFO-1225ye), the conversion of 1,1,1,3,3,3-hexafluoropropane (CF₃CH₂CF₃ or HFC-236fa) into 1,1,3,3,3-pentafluoropropene (CF₃CH═CF₂ or HFO-1225zc), the conversion of 1,1,1,2,3,3-hexafluoropropane (CF₃CF₂CFH₂ or HFC-236cb) into 1,2,3,3,3-pentafluoropropene (CHF═CFCF₃ or HFO-1225ye), the conversion of 1,1,1,2,2-pentafluoropropane (CF₃CF₂CH₃ or HFC-245cb) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), and the conversion of 1,1,1,2,3-pentafluoropropane (CF₃CHFCH₂F or HFC-245eb) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf).

In particular, the halogenated hydrocarbon compound is 1,1,1,2,2-pentafluoropropane (HFC-245cb) for the production of 2,3,3,3-tetrafluoropropene (HFO-1234yf). Otherwise, the halogenated hydrocarbon compound is 1,1,1,3,3-pentafluoropropane (HFC-245fa) for the production of 1,3,3,3-tetrafluoropropene (HFO-1234ze).

In the processes according to the first and the second embodiment, the reaction of said hydrocarbon compound with hydrogen fluoride may be performed in the presence of oxygen or of chlorine.

In a third embodiment, the fluorine distribution in the hydrocarbon compound is modified by isomerizing said hydrocarbon compound in the presence of said catalytic composition, said hydrocarbon compound being a fluorinated hydrocarbon compound.

In a fourth embodiment, the fluorine distribution in the hydrocarbon compound is modified by dismutating said hydrocarbon compound in the gas phase in the presence of said catalytic composition, said hydrocarbon compound being a chlorofluorinated hydrocarbon compound.

The isomerization and dismutation processes of the third and fourth embodiments are successfully performed in the vapor phase in the presence of said catalytic composition.

The fluorinated hydrocarbon compounds that are suitable as starting materials for the isomerization and dismutation processes may be saturated or unsaturated. The saturated fluorinated hydrocarbon compounds that are suitable for the isomerization and dismutation processes include those of general formula C_(n)H_(a)Br_(b)Cl_(c)F_(d), in which n is an integer between 2 and 6, a is an integer between 0 and 13, b is an integer between 0 and 4, c is an integer between 0 and 13, d is an integer between 1 and 13, and the sum of a, b, c and d is equal to 2n+2, provided that a+b+c>1. The unsaturated fluorinated hydrocarbon compounds that are suitable for the isomerization and dismutation processes include those of general formula C_(p)H_(e)Br_(f)Cl_(g)F_(h), in which p is an integer between 2 and 6, e is an integer between 0 and 11, f is an integer between 0 and 2, g is an integer between 0 and 12, h is an integer between 1 and 11, and the sum of e, f, g and h is equal to 2p, provided that the sum e+f+g>1.

The fluorine distribution of a fluorinated hydrocarbon compound is modified by rearranging the H, Br, Cl and F substituents in the molecule (typically a thermodynamically preferential arrangement) while keeping the same number of H, Br, Cl and F substituents, respectively. In the present document, this process is known as isomerization.

The fluorine distribution of a fluorinated hydrocarbon compound is modified by exchanging at least one F substituent of the halogenated hydrocarbon starting material with at least one H, Br and/or Cl substituent of another molecule of the halogenated hydrocarbon starting material, so as to give the formation of one or more halogenated hydrocarbon compounds having a reduced fluorine content, with respect to the halogenated hydrocarbon starting material, and one or more halogenated hydrocarbon compounds having an increased fluorine content, with respect to the halogenated hydrocarbon starting material. In the present document, this process is known as dismutation.

The isomerization and dismutation reactions may take place simultaneously.

Whether an isomerization, a dismutation or both an isomerization and a dismutation are performed, it is possible to modify the fluorine distribution of saturated compounds of formula C_(n)H_(a)Br_(b)Cl_(c)F_(d) and/or of unsaturated compounds of formula C_(p)H_(e)Br_(f)Cl_(g)F_(h) in the presence of a catalyst as disclosed above.

The isomerization and dismutation processes are typically successfully performed at temperatures between approximately 100° C. and 500° C., preferably between approximately 150° C. and approximately 400° C. The contacting time in the reactor is typically from approximately 1 to approximately 120 s, preferably from approximately 5 to approximately 60 s. The isomerization and dismutation reactions may be successfully performed in the presence of an inert gas, such as helium, argon or nitrogen, although this is not preferential. The isomerization and dismutation reactions may be successfully performed in the presence of HF and HCl.

Preferentially, the isomerization processes may be performed using the present catalyst and include the conversion of 1-chloro-1,1-difluoroethane (CH₃CF₂Cl or HCFC-142b) into 1-chloro-2,2-difluoroethane (CH₂ClCF₂H or HCFC-142), the conversion of 1,3-dichloro-1,2,2,3,3-pentafluoropropane (CHClFCF₂CF₂Cl or HCFC-225cb) into 1,1-dichloro-2,2,3,3,3-pentafluoropropane (CHCl₂CF₂CF₃ or HCFC-225ca), the conversion of 2,2-dichloro-1,1,1,3,3-pentafluoropropane (CHF₂CCl₂CF₃ or HCFC-225aa) into 1,1-dichloro-2,2,3,3,3-pentafluoropropane (CHCl₂CF₂CF₃ or HCFC-225ca), the conversion of 1,1,1,2,3-pentafluoropropane (CF₃CHFCH₂F or HFC-245eb) into 1,1,1,2,2-pentafluoropropane (CF₃CF₂CH₃ or HFC-245cb), the conversion of 1,1,1,3,3-pentafluoropropane (CHF₂CH₂CF₃ or HFC-245fa) into 1,1,1,2,3-pentafluoropropane (CF₃CHFCH₂F or HFC-245eb), the conversion of 1,3,3,3-tetrafluoropropene (CHF═CHCF₃ or HFO-1234ze) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf), the conversion of 1,1,3,3-tetrafluoropropene (CF₂═CHCHF₂ or HFO-1234zc) into 1,3,3,3-tetrafluoropropene (CHF═CHCF₃ or HFO-1234ze), the conversion of 1-chloro-3,3,3-trifluoro-1-propene (CHCl═CHCF₃ or HCFO-1233zd) into 2-chloro-3,3,3-trifluoro-1-propene (CH₂═CClCF₃ or HCFO-1233xf) and the conversion of the (Z) isomer of the hydrochlorofluoroolefins into the (E) isomer of the hydrochlorofluoroolefins.

In particular, the (Z) isomers of hydrochlorofluoroolefins are the (Z) isomers of the hydrochlorofluoropropenes and hydrochlorofluorobutenes. Specific examples include the conversion of (Z)-1-chloro-3,3,3-trifluoro-1-propene (CHCl═CHCF₃ or HCFO-1233zd(Z)) into (E)-1-chloro-3,3,3-trifluoro-1-propene (CHCl═CHCF₃ or HCFO-1233zd(E)), the conversion of (Z)-1,3,3,3-tetrafluoropropene (CHF═CHCF₃ or HFO-1234ze(Z)) into (E)-1,3,3,3-tetrafluoropropene (CHF═CHCF₃ or HFO-1234ze(E)), the conversion of (Z)-1,2,3,3,3-pentafluoropropene (CHF═CFCF₃ or HFO-1225ye(Z)) into (E)-1,2,3,3,3-pentafluoropropene (CHF═CFCF₃ or HFO-1225ye(E)) and the conversion of (Z)-1,1,1,4,4,4-hexafluoro-2-butene (CF₃CH═CHCF₃ or HFO-1336mzz(Z)) into (E)-1,1,1,4,4,4-hexafluoro-2-butene (CF₃CH═CHCF₃ or HFO-1336mzz(E)).

Preferentially, the dismutation processes may be performed using the present catalyst and include the conversion of chlorofluoromethane (CH₂ClF or HCFC-31) into difluoromethane (CH₂F₂ or HFC-32) and dichloromethane (CH₂Cl₂ or HCC-30), the conversion of 1-chloro-1,1-difluoroethane (CH₃CClF₂ or HCFC-142b) into 1,1,1-trifluoroethane (CH₃CF₃ or HFC-143a) and 1,1-dichloro-1-fluoroethane (CH₃CCl₂F or HCFC-141b), the conversion of 1-chloro-1,2,2,2-tetrafluoroethane (CF₃CHClF or HCFC-124) into pentafluoroethane (CF₃CHF₂ or HFC-125) and into 2,2-dichloro-1,1,1-trifluoroethane (CF₃CHCl₂ or HCFC-123), the conversion of 1,1,3-trichloro-2,2,3,3-tetrafluoropropane (CHCl₂CF₂CF₂Cl or HCFC-224ca) into 1,1-dichloro-2,2,3,3,3-pentafluoropropane (CHCl₂CF₂CF₃ or HCFC-225ca) and 1,1,3,3-tetrachloro-1,2,2-trifluoropropane (CHCl₂CF₂CCl₂F or HCFC-223ca), the conversion of 1,1,1,3-tetrafluoro-3-chloropropane (CF₃CH₂CHClF or HCFC-244fa) into 1,1,1,3,3-pentafluoropropane (CHF₂CH₂CF₃ or HFC-245fa) and into 1,1,1-trifluoro-3,3-dichloropropane (CF₃CH₂CHCl₂ or HCFC-243fa), the conversion of 1,1,2,3-tetrafluoro-1-chloropropane (CF₂ClCHFCH₂F or HCFC-244ec) into 1,1,1,2,3-pentafluoropropane (CF₃CHFCH₂F or HFC-245eb) and into 1,2,3-trifluoro-1,1-dichloropropane (CFCl₂CHFCH₂F or HCFC-243ed), the conversion of 1,1,2,2-tetrafluoro-1-chloropropane (CF₂ClCF₂CH₃ or HCFC-244cc) into 1,1,1,2,2-pentafluoropropane (CF₃CF₂CH₃ or HFC-245cb) and 1,2,2-trifluoro-1,1-dichloropropane (CFCl₂CF₂CH₃ or HCFC-243cc), the conversion of 3-chloro-2,3,3-trifluoro-1-propene (CH₂═CFCClF₂ or HCFO-1233yf) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf) and into 3,3-dichloro-2,3-difluoro-1-propene (CH₂═CFCFCl₂ or HCFO-1232yf) and the conversion of 3-chloro-1,3,3-trifluoro-1-propene (CHF═CHCClF₂ or HCFO-1233ze) into 1,3,3,3-tetrafluoropropene (CHF═CHCF₃ or HFO-1234ze) and 3,3-dichloro-1,3-difluoro-1-propene (CHF═CHCCl₂F or HCFO-1232ze).

In a fifth embodiment, the fluorine content of the hydrocarbon compound is reduced by reacting said hydrocarbon compound with hydrogen chloride in the gas phase in the presence of said catalytic composition, said hydrocarbon compound being a halogenated hydrocarbon compound.

The fluorinated hydrocarbon compounds that are suitable as starting materials for the process of this embodiment may be saturated or unsaturated. The saturated halogenated hydrocarbon compounds that are suitable for the chlorodefluorination processes according to this invention include those of general formula C_(n)H_(a)Cl_(c)F_(d), in which n is an integer between 1 and 6, a is an integer between 0 and 13, c is an integer between 0 and 13, d is an integer between 1 and 13, and the sum of a, c and d is equal to 2n+2. The unsaturated halogenated hydrocarbon compounds that are suitable for the chlorodefluorination processes according to this invention include those of general formula C_(p)H_(e)Cl_(g)F_(h), in which p is an integer between 2 and 6, e is an integer between 0 and 11, g is an integer between 0 and 12, h is an integer between 1 and 11, and the sum of e, g and h is equal to 2p.

The chlorodefluorination reactions are typically performed at temperatures of approximately 250° C. to 450° C., preferably of approximately 300° C. to approximately 400° C. The contacting time in the reactor is typically from approximately 1 to approximately 120 s. Needless to say, contact times of approximately 5 to approximately 60 s are possible. The reactions are ideally performed at atmospheric or greater pressure.

The chlorodefluorinations involving saturated halogenated hydrocarbons are particularly worthy of interest. The mole ratio of HCl to the saturated halogenated hydrocarbon compound typically lies between approximately 1:1 and approximately 100:1, preferably from approximately 3:1 to approximately 50:1, and ideally from approximately 4:1 to approximately 30:1. In general, with a given catalytic composition, the higher the temperature, the longer the contact time, the greater the mole ratio of HCl to the saturated halogenated hydrocarbon compound and the greater the conversion of the compounds having a low fluorine content. The above variables can be balanced with respect to each other in order to maximize the formation of chlorinated products.

The product of the chlorodefluorination reactions typically comprises HCl and unreacted HF, unconverted starting material and saturated halogenated hydrocarbon compounds having a lower fluorine content than the starting material as a result of the substitution of one or more fluorine substituents with chlorine.

The reaction products obtained via the processes described in detail in any one of the first five embodiments may be separated via conventional techniques, such as with combinations including, in a nonlimiting manner, washing, settling or distillation. Some of the products of the various embodiments of this invention can form one or more azeotropes with each other or with HF.

The processes disclosed in the present invention may include, in addition, a step of regeneration of said catalytic composition in the presence of a regeneration stream comprising a stream of air/oxidant. The oxidant may be oxygen, air, a mixture of oxygen and nitrogen, chlorine or a mixture of chlorine and nitrogen. When the regeneration is performed with air or a mixture of oxygen and nitrogen, the proportion of oxygen may range from 5 mol % to 100 mol %, relative to the mixture of oxygen and nitrogen. The regeneration step may be performed in the presence of a regeneration stream containing (a) oxygen or air or an oxygen/nitrogen mixture or chlorine and (b) HF. Advantageously, the regeneration stream will contain at least 1 mol % of oxygen, relative to the total regeneration stream. The proportion of oxygen may range from 2 mol % to 98 mol %, relative to the total amount expressed in moles of oxygen and HF, and from 20 mol % to 100 mol %, relative to the total amount expressed in moles of oxygen and nitrogen. The regeneration step is successfully performed at a temperature of 250 to 500° C., preferably of 300 to 450° C., more preferentially of 350 to 400° C. The regeneration step may be successfully performed with a contact time of 1 to 200 s, preferably of 1 to 150 s, more preferentially of 5 to 100 s, and for a period of time of 1 to 1500 hours, preferably of 2 to 1000 hours, more preferentially of 4 to 500 hours, ideally of 10 to 200 hours and in particular of 15 to 150 hours. The regeneration step may be successfully performed under a pressure ranging from atmospheric pressure to 20 bara. In particular, the regeneration step may be successfully performed at a temperature of 250 to 500° C., with a contact time of 1 to 200 s, for 10 to 200 hours and under a pressure between atmospheric pressure and 20 bara.

The processes disclosed in the present invention may comprise, in addition, the step of activation of said catalytic composition in the presence of an air/oxidant stream. Before use, it is preferable for the catalyst to be subjected to a step of activation with air, oxygen or chlorine and/or HF. For example, the catalyst is preferentially subjected to activation with air or oxygen and HF at a temperature between 100 and 500° C., preferably between 250 and 500° C. and in particular between 300 and 400° C. The duration of activation is preferentially from 1 to 200 hours and in particular from 1 to 50 hours. This activation may be followed by a final step of fluorination activation in the presence of an oxidant, HF and hydrocarbon compounds. The HF/hydrocarbon compound mole ratio ranges from 2 to 40 and the oxidant/hydrocarbon compound mole ratio ranges from 0.04 to 25. The temperature of the final step of fluorination activation may range from 300 to 400° C., preferably for a duration of 6 to 100 hours.

Otherwise, the present invention may also provide a process for modifying the chlorine distribution in a hydrocarbon compound in the presence of said catalytic composition. The chlorine content of the hydrocarbon compound is reduced by dehydrochlorination of said hydrocarbon compound in the presence of said catalytic composition, said hydrocarbon compound being a chlorinated hydrocarbon compound. The chlorinated hydrocarbon compounds that are suitable as starting materials for the dehydrochlorination process are typically saturated. The saturated chlorinated hydrocarbon compounds include those of general formula C_(n)H_(a)Cl_(d), in which n is an integer between 2 and 6, a is an integer between 1 and 12, d is an integer between 1 and 13, and the sum of a and d is equal to 2n+2. The process according to this alternative embodiment may be performed in a reactor comprising a catalytic bed containing a catalyst and according to the following operating conditions:

-   -   contact time of 1 to 100 s, preferably of 2 to 75 s, in         particular of 3 to 50 s;     -   pressure between atmospheric pressure and 20 bara, preferably         from 2 to 18 bara, more preferentially from 3 to 15 bara;     -   temperature, preferably of the catalytic bed, of 200 to 450° C.,         preferably of 250 to 400° C., more preferentially of 280 to 380°         C.

The process may be performed for a period of time of 10 to 8000 hours, preferably of 50 to 5000 hours, more preferentially of 70 to 1000 hours.

The product of the dehydrochlorination reaction consists of HCl and the unsaturated fluorinated hydrocarbon compound resulting from the loss of HCl by the initial reagent. Specific examples of vapor-phase dehydrochlorination reactions may be performed using said catalytic composition include the conversion of 1-chloro-2,2-difluoroethane (CH₂ClCF₂H or HCFC-142) into 1,1-difluoroethylene (CH₂═CF₂ or HFO-1132a), the conversion of 1,1,1,3-tetrafluoro-3-chloropropane (CF₃CH₂CHClF or HCFC-244fa) into 1,3,3,3-tetrafluoropropene (CHF═CHCF₃ or HFO-1234ze), the conversion of 1,1,1-trifluoro-3,3-dichloropropane (CF₃CH₂CHCl₂ or HCFC-243fa) into 1-chloro-3,3,3-trifluoro-1-propene (CHCl═CHCF₃ or HCFO-1233zd), the conversion of 2,3-dichloro-1,1,1-trifluoropropane (CF₃CHClCH₂Cl or HCFC-243db) into 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HFCO-1233xf), the conversion of 2-chloro-1,1,1,2-tetrafluoropropane (CF₃CFClCH₃ or HCFC-244bb) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf) and the conversion of 1,1,1,4,4,4-hexafluoro-2-chlorobutane (CF₃CHClCH₂CF₃ or HFC-346mdf) into 1,1,1,4,4,4-hexafluoro-2-butene (CF₃CH═CHCF₃ or HFO-1336mzz). The process for modifying the chlorine distribution in a hydrocarbon compound may be successfully performed simultaneously with a process for modifying the fluorine distribution in another hydrocarbon compound, for example by increasing or reducing the fluorine content in said other hydrocarbon compound, as described in detail above with reference to the first embodiment and the second embodiment. Consequently, the conversion of 2-chloro-1,1,1,2-tetrafluoropropane (CF₃CFClCH₃ or HCFC-244bb) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf) may be performed with the present catalytic composition simultaneously with the conversion of 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf).

In a sixth embodiment, the fluorine content of a first hydrocarbon compound is increased by reacting said first hydrocarbon compound with hydrogen fluoride in the gas phase in the presence of said catalytic composition, the first hydrocarbon compound being a saturated halogenated hydrocarbon or an unsaturated halogenated hydrocarbon or an unsaturated hydrocarbon, and the fluorine content of a second hydrocarbon compound is reduced by dehydrofluorinating said second hydrocarbon compound in the presence of said catalytic composition, said second hydrocarbon compound being a fluorinated hydrocarbon compound. The first hydrocarbon compound, which is a saturated halogenated hydrocarbon or an unsaturated halogenated hydrocarbon or an unsaturated hydrocarbon, is defined above with reference to the first embodiment. The second hydrocarbon compound is defined above with reference to the second embodiment. The fluorination of the first hydrocarbon compound and the dehydrofluorination of the second hydrocarbon compound are preferentially performed simultaneously.

The process according to the sixth embodiment may be performed in a reactor comprising a catalytic bed containing a catalyst and according to the following operating conditions:

-   -   an HF/hydrocarbon compound mole ratio of 1:1 to 150:1,         preferably of 2:1 to 125:1, more preferentially of 3:1 to 100:1;     -   a contact time of 1 to 100 s, preferably of 2 to 75 s, in         particular of 3 to 50 s;     -   a pressure between atmospheric pressure and 20 bara, preferably         between 2 and 18 bara, more preferentially between 3 and 15         bara;     -   a temperature (of the catalytic bed) between 200 and 450° C.,         preferably between 250 and 400° C., more preferentially between         280° C. and 380° C.

The process may be successfully performed over a time of between 10 and 8000 hours, preferably between 50 and 5000 hours, more preferentially between 70 and 1000 hours.

An oxidant, such as oxygen or chlorine, may be added during the process. The mole ratio of the oxidant to the hydrocarbon compound may be between 0.005 and 2, preferably between 0.01 and 1.5. The oxidant may be pure oxygen, air, or a mixture of oxygen and nitrogen.

The products of the reaction are those described in detail with reference to the first embodiment and the second embodiment. In particular, the catalytic composition is useful for the conversion of 1,1,1,2,3-pentachloropropane (CCl₃CHClCH₂Cl or HCC-240db) into 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf) or the conversion of 1,1,1,2,3-pentachloropropane (CCl₃CHClCH₂Cl or HCC-240db) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf) or the conversion of 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf) and the conversion of 1,1,1,2,2-pentafluoropropane (CF₃CF₂CH₃ or HFC-245cb) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf) or the conversion of 1,1,1,2,3-pentafluoropropane (CF₃CHFCH₂F or HFC-245eb) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf). In particular, the catalytic composition is useful for the conversion of 2-chloro-3,3,3-trifluoro-1-propene (CF₃CCl═CH₂ or HCFO-1233xf) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf) and the conversion of 1,1,1,2,2-pentafluoropropane (CF₃CF₂CH₃ or HFC-245cb) into 2,3,3,3-tetrafluoropropene (CF₃CF═CH₂ or HFO-1234yf).

The process according to the sixth embodiment may be performed in a reactor comprising a catalytic bed containing a catalyst and according to the following operating conditions:

-   -   an HF/hydrocarbon compound mole ratio of 1:1 to 150:1,         preferably of 2:1 to 125:1, more preferentially of 3:1 to 100:1;     -   a contact time of 1 to 100 s, preferably of 2 to 75 s, in         particular of 3 to 50 s;     -   a pressure between atmospheric pressure and 20 bara, preferably         between 2 and 18 bara, more preferentially between 3 and 15         bara;     -   a temperature, preferably of the catalytic bed, between 200 and         450° C., preferably between 250 and 400° C., more preferentially         between 280° C. and 380° C.

The process may be successfully performed over a time of between 10 and 8000 hours, preferably between 50 and 5000 hours, more preferentially between 70 and 1000 hours.

EXAMPLE

Three metal coupons of different constitution, corresponding to the material M2 as described in the present patent application, were subjected to fluorination operating conditions in order to determine their rate of corrosion. The corrosion coupons were installed for 400 days in a fluorination reactor alternating fluorination reactions in the presence of hydrofluoric acid, a chromium oxyfluoride catalyst and 1,1,1,2,3-pentachloropropane (temperature of 350° C., 4 bara) and catalyst regeneration reactions. Coupon A consists of a material comprising more than 99% by weight of nickel. Coupon B consists of a material comprising 32% by weight of nickel. Coupon C consists of a material comprising 11% by weight of nickel. The rate of corrosion of coupons A-C is determined after the 400 days by microscopic observation. The data are collated in Table 1 below.

TABLE 1 Coupon A Coupon B Coupon C (Invention) (comparative) (comparative) wt % Ni >99 wt % 32 wt % 11 wt % Rate of corrosion 0 μm/year* 4 μm/year 130 μm/year *The value “0 μm/year” means that no corrosion was observed

The metal coupon A corresponding to a material M2 according to the present patent application and comprising more than 99% by weight of nickel has very substantial stability over time, even under harsh operating conditions.

Complementary tests also made it possible to show that a material comprising iron (>98% by weight and less than 0.2% carbon, corresponding to a material M1 according to the present invention) had excellent heat stability, even at temperatures above 600° C. 

1-13. (canceled)
 14. A process for modifying the fluorine distribution in a hydrocarbon compound, comprising a step of contacting a hydrocarbon compound and a catalytic composition comprising a chromium-based catalyst in a reactor, said reactor made of a material comprising a base layer made of a material M1 and an inner layer made of a material M2, said base layer and said inner layer being laid against each other, wherein the material M2 comprises at least 80% by weight of nickel on the basis of the total weight of the material M2.
 15. The process as claimed in claim 14, wherein the material M1 comprises iron and less than 0.2% of carbon on the basis of the total weight of the material M1.
 16. The process as claimed in claim 14, wherein the material M2 comprises less than 1% of iron on the basis of the total weight of the material M2.
 17. The process as claimed in claim 14, wherein the material M2 comprises less than 1% of manganese on the basis of the total weight of the material M2.
 18. The process as claimed in claim 14, wherein the material M2 comprises less than 1% by weight of titanium and/or less than 1% by weight of niobium on the basis of the total weight of the material M2.
 19. The process as claimed in claim 14, wherein said hydrocarbon compound is of formula (I) CX(Y)₂—CX(Y)_(m)—CH_(m)XY, in which X and Y independently represent H, F or Cl and m=0 or 1 with at least one from among X or Y which is Cl or F.
 20. The process as claimed in claim 19, wherein the hydrocarbon compound is selected from the group consisting of tetrachloropropene, chlorotrifluoropropene, pentachloropropane, dichlorotrifluoropropane, trichlorodifluoropropane, tetrafluorochloropropane, tetrachlorofluoropropane, dichlorodifluoropropene, trichlorofluoropropene, pentafluoropropane and mixtures thereof.
 21. The process as claimed in claim 14, wherein the fluorine content of the hydrocarbon compound is increased by reacting said hydrocarbon compound with hydrogen fluoride in the gas phase in the presence of said catalytic composition, the hydrocarbon compound being a saturated halogenated hydrocarbon or an unsaturated halogenated hydrocarbon or an unsaturated hydrocarbon.
 22. The process as claimed in claim 14, wherein the fluorine content of the hydrocarbon compound is reduced by dehydrofluorination of said hydrocarbon compound in the presence of said catalytic composition, said hydrocarbon compound being a fluorinated hydrocarbon compound.
 23. The process as claimed in claim 14, wherein the fluorine distribution of the hydrocarbon compound is modified by isomerizing said hydrocarbon compound in the presence of said catalytic composition, said hydrocarbon compound being a fluorinated hydrocarbon compound.
 24. The process as claimed in claim 14, wherein the fluorine distribution of the hydrocarbon compound is modified by dismutating said hydrocarbon compound in the gas phase in the presence of said catalytic composition, said hydrocarbon compound being a chlorofluorinated hydrocarbon compound.
 25. The process as claimed in claim 14, wherein the fluorine content of the hydrocarbon compound is reduced by reacting said hydrocarbon compound with hydrogen chloride in the gas phase in the presence of said catalytic composition, said hydrocarbon compound being a halogenated hydrocarbon compound containing at least one fluorine atom.
 26. The process as claimed in claim 14, wherein the fluorine content of a first hydrocarbon compound is increased by reacting said first hydrocarbon compound with hydrogen fluoride in the gas phase in the presence of a catalytic composition comprising a chromium-based catalyst, the first hydrocarbon compound being a saturated halogenated hydrocarbon or an unsaturated halogenated hydrocarbon or an unsaturated hydrocarbon, and in which the fluorine content of a second hydrocarbon compound is reduced by dehydrofluorinating said second hydrocarbon compound in the presence of said catalytic composition, said second hydrocarbon compound being a fluorinated hydrocarbon compound.
 27. The process of claim 20, wherein the hydrocarbon compound is selected from the group consisting of 2-chloro-3,3,3-trifluoro-1-propene (HFCO-1233xf), 2,3-dichloro-1,1,1-trifluoropropane (HCFC-243db), 1,1,1,1,2,3-pentachloropropane (HCC-240db), 1,1,2,2,3-pentachloropropane (HCC-240aa), 1,1,1,3,3-pentachloropropane (HCC-240fa), 1,1,2,3-tetrachloro-1-propene (HCO-1230xa), 2,3,3,3-tetrachloro-1-propene (HCO-1230xf), 1,1,3,3-tetrachloro-1-propene (HCO-1230za), 1,3,3,3-tetrachloro-1-propene (HCO-1230zd), 1,1,1,2,2-pentafluoropropane (HFC-245cb) and 1-chloro-3,3,3-trifluoro-1-propene (HCFO-1233zd). 